Embodiments include a method and apparatus for producing synthesis gas in a catalytic partial oxidation reactor by adding hydrogen to the reactor feed stream.
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1. A method for conducting a partial oxidation reaction, the method comprising:
providing a catalytic partial oxidation reactor;
operating a dehydrogenation reaction so as to produce a hydrogen stream;
providing a feed stream comprising a hydrocarbon-containing gas, an oxygen-containing gas, and a hydrogen-containing gas, wherein at least a portion of said hydrogen-containing gas comprises at least a portion of the hydrogen produced in the dehydrogenation reaction; and
feeding the feed stream through the partial oxidation reactor;
operating the partial oxidation reactor at conditions effective to partially oxidize at least a portion of the hydrocarbon-containing gas to a product stream comprising synthesis gas such that, the hydrogen fed to the catalytic partial oxidation reactor increases the H2:CO molar ratio in the product stream.
22. A method of convening a light hydrocarbon-containing gas to higher hydrocarbons, the method comprising:
providing a partial oxidation reactor feed stream comprising a light hydrocarbon-containing gas and an oxygen-containing gas;
providing a catalytic partial oxidation reactor;
feeding the partial oxidation reactor feed stream into the partial oxidation reactor;
operating the partial oxidation reactor at conditions which favor the partial oxidation of the light hydrocarbon to a product stream comprising synthesis gas;
providing a hydrocarbon synthesis reactor;
feeding at least a portion of the partial oxidation reactor product stream to the Fischer-Tropsch reactor as the hydrocarbon synthesis feed stream;
operating the hydrocarbon synthesis reactor at conditions which favor the conversion of the hydrocarbon synthesis feed stream to higher hydrocarbons;
removing a gas effluent stream from the hydrocarbon synthesis reactor;
obtaining a recycle stream comprising at least a portion of the gas effluent from the hydrocarbon synthesis reactor and an amount of hydrogen from produced in a dehydrogenation reactor; and
recycling at least a portion of the recycle stream to the partial oxidation reactor.
10. A method for convening a light hydrocarbon-containing gas to higher hydrocarbons, the method comprising:
providing a partial oxidation reactor feed stream comprising a light hydrocarbon-containing gas and an oxygen-containing gas;
providing a catalytic partial oxidation reactor;
feeding the partial oxidation reactor feed stream into the catalytic partial oxidation reactor;
operating the catalytic partial oxidation reactor at conditions which favor the partial oxidation of the light hydrocarbon to a product stream comprising synthesis gas;
providing a hydrocarbon synthesis reactor;
feeding at least a portion of the catalytic partial oxidation reactor product stream to the hydrocarbon synthesis reactor as a hydrocarbon synthesis feed stream;
operating the hydrocarbon synthesis reactor at conditions which favor the conversion of the hydrocarbon synthesis feed stream to higher hydrocarbons;
removing a gas effluent stream from the hydrocarbon synthesis reactor;
directly or indirectly recycling at least a portion of the effluent stream from the hydrocarbon synthesis reactor to the catalytic partial oxidation reactor, wherein the portion of the recycled effluent stream fed to the catalytic partial oxidation reactor comprises hydrogen and carbon monoxide;
including in the hydrogen-containing gas a hydrogen stream produced by dehydrogenation of alkanes; and
feeding at least a portion of the recycled effluent stream through the catalytic partial oxidation reactor such that the hydrogen fed to the catalytic partial oxidation reactor increases the H2:CO molar ratio of its product stream.
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This application is a continuation-in-part of application Ser. No. 10/299,193, filed Nov. 19, 2002, now is abandoned.
The present invention relates to a process for the preparation of synthesis gas, i.e., a mixture of carbon monoxide and hydrogen, from a hydrocarbon feedstock. Particularly, the present invention relates to adding hydrogen to the feed stream of a (CPOX) partial oxidation reactor, preferably a catalytic partial oxidation reactor.
Large quantities of natural gas are available in many areas of the world, and natural gas is predicted to outlast oil reserves by a significant margin. However, a significant amount of natural gas is situated in areas that are geographically remote from population and industrial centers. The costs of compression, transportation, and storage make its use economically unattractive. To improve the economics of natural gas use, much research has focused on the use of methane, the main component of natural gas, as a starting material for the production of higher hydrocarbons and hydrocarbon liquids, which are more easily transported and thus more economical. The conversion of methane to higher hydrocarbons or hydrocarbon liquids is typically carried out in two steps. In the first step, methane is converted into a mixture of carbon monoxide and hydrogen (i.e., synthesis gas or syngas). In a second step, the syngas is converted into the higher hydrocarbons via a process such as Fischer-Tropsch synthesis or alcohols via alcohol synthesis. An acceptable example of Fischer-Tropsch synthesis is disclosed in U.S. Pat. No. 6,333,294 to Chao et al., incorporated herein by reference.
Current industrial use of methane or natural gas as a chemical feedstock proceeds by the initial conversion of the feedstock to carbon monoxide and hydrogen by either steam reforming (the most widespread process), dry reforming, autothermal reforming, partial oxidation or catalytic partial oxidation. Examples of these processes are disclosed in Gunardson, Harold, INDUSTRIAL GASES IN PETROCHEMICAL PROCESSING 41-80 (1998), incorporated herein by reference. Steam reforming, dry reforming, and catalytic partial oxidation proceed according to the following reactions respectively: ##STR00001##
As is shown schematically in
After the syngas is reacted into higher hydrocarbons (if reactor 2 is a Fischer-Tropsch reactor) or alcohols (if reactor 2 is an alcohol synthesis reactor) the gas effluent 50 is separated from the liquid product stream 30. The liquid product stream goes on for further processing (not shown). If reactor 2 is a Fischer-Tropsch reactor, the gas effluent 50 generally comprises methane, unreacted H2, unreacted CO and other impurities such as CO2 and other light hydrocarbons. If reactor 2 is an alcohol synthesis reactor, gas effluent generally comprises CO and H2.
It would generally be desirable to eliminate or reduce the amount of supplemental hydrogen added in supplemental hydrogen stream 40. Additionally, it would be desirable to recycle a Fischer-Tropsch effluent stream rich in methane to a CPOX reactor without the need to separate hydrogen from the effluent stream.
In preferred embodiments of the present invention, there are shown methods and apparatus for conducting a partial oxidation reaction in a reactor having a feed stream comprising a hydrogen-containing gas that has been preferably been recycled from the FT or other area within the GTL plant, an oxygen-containing gas, and a gaseous hydrocarbon.
In a preferred embodiment, shown in
Even with the hydrogen in gas effluent stream 140 or if the H2:CO ratio in gas effluent stream 140 is lower than that needed to conduct the Fischer-Tropsch reactions, the catalytic partial oxidation product stream 120 may have an H2:CO ratio which is lower than that needed to conduct the Fischer-Tropsch reactions in Fischer-Tropsch reactor 102. If that is the case, optional supplemental hydrogen stream 150 may be added to product stream 120 before it is fed into the Fischer-Tropsch reactor. It is contemplated that in many instances, the amount of supplemental hydrogen 150 needed will be greatly reduced, or even preferably eliminated, from that needed in the conventional system of FIG. 1. Thus, greatly reducing or eliminating the cost associated with providing that supplemental hydrogen. Additionally, even if the need for supplemental hydrogen is not reduced (e.g., because the H2:CO ratios in the recycle stream is too low), the ability to recycle the methane from the FT effluent without the use of expensive separation techniques is extremely valuable.
In preferred embodiments the hydrogen is provided by a recycle stream from the Fischer-Tropsch reactor (e.g., gas effluent stream 140). A recycle stream could also come from other areas of the GTL plan such as product upgrading or anywhere hydrogen is produced or even from bottled or trucked-in hydrogen. Product upgrading can comprise, but is not limited to, the following processes, hydrocracking, hydroprocessing, hydrotreating, and the like, exemplary examples of which are know to one of ordinary skill in the art. The hydrogen can also come from a plant which dehydrogenates alkanes to produce olefins and hydrogen (e.g., ethane to ethylene), examples of which are well known in the art. In addition to hydrogen, CO, methane, light hydrocarbons, CO2, and/or inerts such as, by way of example only, N2 and Ar, could also be present. Applicants expect that the presence of carbon monoxide and carbon dioxide in the recycle stream will not have a substantial effect on the overall efficiency of the partial oxidation reactor. For example, Applicants believe that the introduction of carbon monoxide and carbon dioxide into the partial oxidation feed will have a slight negative effect (about a 2-4% decrease in conversion), however, it is expected that any negative effect will be more than outweighed by the elimination or substantial reduction in the need for the supplemental hydrogen, the need to separate the methane in the FT effluent, or the wasted methane in the FT effluent.
A primary benefit to this invention is to reduce the complexity of FT tail gas handling without destroying the unconverted H2 and CO. The separation of H2, inerts such as N2 and Ar, CO and methane is difficult. Optimally, one would want to recycle H2 and CO to the FT, purge the N2 and Ar inerts and recycle methane to the syngas step. Complexity, cost and loss product to thermodynamics preclude this. The fact that the CPOX can handle the described recycle without destroying H2 and CO is unique and very advantageous.
Experiments were conducted on a CPOX catalyst system with a feed gas pre-heat of 300° C. Tests reactions were run with the following feed compositions using bottled hydrogen and achieved the listed approximate H2:CO molar ratios in the product stream (Table 1). In Run No. 1, the total feed stream flow rate was 3.5 SLPM. In all other runs, the total feed stream flow rate was 5.0 SLPM.
TABLE 1
Products
Bottled
Stream H2:CO
Run No.
CH4 mol %
O2 mol %
H2 mol %
molar ratio
1
64
36
0
≈1.97
2
64
36
0
≈2.02
3
62
36
4
≈2.09
4
60
33
7
≈2.14
5
58
32
10
≈2.19
6
56
31
13
≈2.25
As can be easily determined from Table 1, the addition of bottled hydrogen to the partial oxidation feed stream is shown to increase the H2:CO molar ratio in the partial oxidation product stream.
The term “catalyst system” as used herein means any acceptable system for catalyzing the desired reaction in the reaction zone. By way of example only, a CPOX catalyst usually includes a support and a catalyst. The support may be, for example, particulates, pills, beads, granules, pellets, rings, monoliths, ceramic honeycomb structures, wire gauze, or any other suitable supports in any acceptable manufactured shape such as those listed herein. The CPOX catalyst may be selected from the group consisting of nickel, samarium, rhodium, cobalt, platinum, rhodium-samarium, platinum-rhodium Ni—MgO, Group VIII metals, nickel-based catalysts, combinations thereof, or any other catalysts mentioned herein or as is well known in the art. The above-exemplified examples of supports and catalysts are only examples. There are a plethora of catalysts systems known in the art which would be acceptable and are contemplated to fall within the scope of the present invention, such as those disclosed in STRUCTURED CATALYSTS AND REACTORS 179-208, 599-615 (Andrzej Cybulski and Jacob A. Moulijn eds. 1998), incorporated herein by reference.
A stream is directly recycled, if it is sent from its source to its destination without being subjected to any processing which changes its composition. Conversely, a stream is indirectly recycled if it is subjected to composition changing processing after leaving its source but before arriving at its destination.
Should the disclosure of any of the patents and publications that are incorporated herein by reference conflict with the present specification to the extent that it might render a term unclear, the present specification shall take precedence.
Without further elaboration, it is believed that one skilled in the art can, using the description herein, utilize the present invention to its fullest extent. The embodiments herein are to be construed as illustrative, and not as constraining the disclosure in any way whatsoever.
Carmichael, Lisa M., Landis, Stephen R., Ricketson, Kevin L., Ruddy, II, Thomas R.
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| Jan 08 2003 | CARMICHAEL, LISA M | Conoco INC | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 013737 | /0976 | |
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| Jan 21 2003 | RUDDY, THOMAS R II | Conoco INC | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 013737 | /0976 |
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